CN112246071A - Torch gas compression and desulfurization integrated process and system thereof - Google Patents
Torch gas compression and desulfurization integrated process and system thereof Download PDFInfo
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- CN112246071A CN112246071A CN202011053442.4A CN202011053442A CN112246071A CN 112246071 A CN112246071 A CN 112246071A CN 202011053442 A CN202011053442 A CN 202011053442A CN 112246071 A CN112246071 A CN 112246071A
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- 238000006477 desulfuration reaction Methods 0.000 title claims abstract description 127
- 230000023556 desulfurization Effects 0.000 title claims abstract description 127
- 238000007906 compression Methods 0.000 title claims abstract description 53
- 230000006835 compression Effects 0.000 title claims abstract description 49
- 238000000034 method Methods 0.000 title claims abstract description 30
- 239000007788 liquid Substances 0.000 claims abstract description 184
- 150000001412 amines Chemical class 0.000 claims abstract description 168
- 239000006096 absorbing agent Substances 0.000 claims abstract description 61
- 238000012546 transfer Methods 0.000 claims abstract description 35
- 239000007921 spray Substances 0.000 claims abstract description 14
- 238000001816 cooling Methods 0.000 claims abstract description 9
- 238000001704 evaporation Methods 0.000 claims description 16
- 230000008020 evaporation Effects 0.000 claims description 16
- 238000005507 spraying Methods 0.000 claims description 9
- CRVGTESFCCXCTH-UHFFFAOYSA-N methyl diethanolamine Chemical compound OCCN(C)CCO CRVGTESFCCXCTH-UHFFFAOYSA-N 0.000 claims description 8
- 238000010521 absorption reaction Methods 0.000 abstract description 9
- 238000005728 strengthening Methods 0.000 abstract description 4
- 239000007789 gas Substances 0.000 description 100
- 230000008929 regeneration Effects 0.000 description 12
- 238000011069 regeneration method Methods 0.000 description 12
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- 229930195733 hydrocarbon Natural products 0.000 description 8
- 150000002430 hydrocarbons Chemical class 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 7
- 229910000037 hydrogen sulfide Inorganic materials 0.000 description 7
- 239000000498 cooling water Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002283 diesel fuel Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 3
- 239000002737 fuel gas Substances 0.000 description 3
- 238000011084 recovery Methods 0.000 description 3
- 238000011160 research Methods 0.000 description 3
- 125000004122 cyclic group Chemical group 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 238000000889 atomisation Methods 0.000 description 1
- 238000003889 chemical engineering Methods 0.000 description 1
- 238000001311 chemical methods and process Methods 0.000 description 1
- 230000003009 desulfurizing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 230000018109 developmental process Effects 0.000 description 1
- 230000009977 dual effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 230000016507 interphase Effects 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 238000000926 separation method Methods 0.000 description 1
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1406—Multiple stage absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1412—Controlling the absorption process
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1418—Recovery of products
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1425—Regeneration of liquid absorbents
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/1456—Removing acid components
- B01D53/1468—Removing hydrogen sulfide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
- B01D53/18—Absorbing units; Liquid distributors therefor
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2252/00—Absorbents, i.e. solvents and liquid materials for gas absorption
- B01D2252/20—Organic absorbents
- B01D2252/204—Amines
- B01D2252/2041—Diamines
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- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
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Abstract
The invention discloses a flare gas compression and desulfurization integrated process and a system thereof, wherein the flare gas compression and desulfurization integrated process comprises the following steps: a pre-desulfurization step; a compression step; a cooling step; a step of super-gravity desulfurization; and (4) flashing. In the step of the supergravity desulfurization, the torch gas and the desulfurization amine liquid are contacted and transferred in the supergravity machine, so that the supergravity desulfurization is realized. The invention adopts the desulfurized amine liquid as the spray liquid, and simultaneously arranges the pre-absorber, the hypergravity machine and other strengthening mass transfer equipment at the compression part, and completes the absorption process at the compression part, thereby not needing to arrange an absorption tower, simplifying the process flow, reducing the occupied area of the equipment and improving the desulfurization efficiency.
Description
Technical Field
The invention relates to a technology for compressing and desulfurizing torch gas with corrosive gases such as hydrogen sulfide and the like in an oil refining production process.
Background
The refinery flare gas is generally merged into a fuel gas pipe network for recycling after being pressurized by a compressor, and because the medium gas contains a certain amount of hydrogen sulfide, the medium gas needs to be desulfurized before being merged into the fuel gas pipe network. At present, the recovery and utilization of flare gas mainly adopt a treatment process of pressurization and wet desulfurization of an N-Methyldiethanolamine (MDEA) solution by an oil-free process screw compressor, but the following problems exist in actual operation and related research:
1. the compression and desulfurization devices are mutually independent, and the equipment investment and energy consumption are large. In order to improve the desulfurization effect, the design pressure of the outlet of the compressor and the consumption of the desulfurization solution in the absorption process are gradually increased, so that the equipment investment and the energy consumption of the device are increased; in addition, the traditional compression process is sprayed with diesel oil for cooling, and continuous consumption caused by volatilization of the diesel oil and separation efficiency exists;
2. the wet desulphurization efficiency is low. At present, a refinery mainly adopts a plate tower or a packed tower for absorption desulfurization, the efficiency is relatively low, and the amine liquid regeneration energy consumption is high. Chemical process strengthening is one of the prior chemical engineering development technologies at present, the mass transfer effect can be improved and the equipment volume can be reduced through strengthening, but related technologies are less applied to a flare gas recovery system;
3. the related domestic patents mainly aim at the research of the compression process or the desulfurization process independently, and the research of the compression and desulfurization integrated process is less. A refinery gas compression and desulfurization process (application publication No. CN 104307341A) firstly proposes that an N-Methyldiethanolamine (MDEA) solution for absorption desulfurization is cited as a compressor spray liquid, but two units of compression and desulfurization are still kept in the process, and a further optimization space exists.
Disclosure of Invention
The technical problem to be solved by the invention is to provide a flare gas compression and desulfurization integrated process and a flare gas compression and desulfurization integrated system, which do not need to adopt a special desulfurization device and have higher desulfurization efficiency.
According to a first embodiment of the invention, there is provided a flare gas compression and desulfurization integrated process comprising the steps of:
a pre-desulfurization step:
atomizing and spraying the desulfurized amine liquid into a pre-absorber, and contacting and transferring mass with torch gas introduced into the pre-absorber to perform pre-desulfurization;
a compression step:
outputting the torch gas and the atomized desulfurized amine liquid in the pre-absorber to a compressor for compression;
and (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor enter a cooler, and are output after exchanging heat with a cold source input into the cooler;
a hypergravity desulfurization step:
inputting the cooled flare gas, the desulfurized amine liquid and the supplemented desulfurized amine liquid into a first hypergravity machine, contacting and transferring the flare gas and the desulfurized amine liquid in the first hypergravity machine to realize hypergravity desulfurization, and outputting the desulfurized flare gas from the first hypergravity machine;
a flash evaporation step:
and (3) flashing the desulfurized amine liquid from the first hypergravity machine through a flash tank.
According to a first embodiment of the invention, there is also provided a flare gas compression and desulfurization system, comprising a pre-absorber, a compressor, a cooler, a first hypergravity machine and a flash tank; the pre-absorber is provided with a torch gas inlet, an amine liquid inlet and an amine liquid outlet; the amine liquid inlet is provided with an atomizing nozzle so as to atomize the desulfurized amine liquid flowing into the amine liquid inlet and then spray the atomized desulfurized amine liquid into the pre-absorber; the inlet of the compressor is communicated with the outlet of the pre-absorber and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber; the cooler is provided with a cold side inlet and a cold side outlet for the cold source to enter and exit, and is used for carrying out heat exchange on the torch gas and the desulfurized amine liquid output by the compressor and the cold source; a first inlet of the first hypergravity machine is communicated with a hot side outlet of the cooler, a second inlet of the first hypergravity machine is used for receiving supplemented desulfurization amine liquid, the first hypergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the first hypergravity machine, the hypergravity desulfurization is realized, and the desulfurized flare gas is output from a first outlet of the first hypergravity machine; and the inlet of the flash tank is communicated with the second outlet of the first hypergravity machine, and the flash tank is used for flashing the desulfurized amine liquid output by the first hypergravity machine.
According to a second embodiment of the present invention, there is provided an integrated flare gas compression and desulfurization process comprising the steps of:
a pre-desulfurization step:
respectively atomizing and spraying the first path of desulfurized amine liquid and the second path of desulfurized amine liquid from a second hypergravity machine into a pre-absorber, and contacting and transferring mass with torch gas introduced into the pre-absorber to perform pre-desulfurization;
a compression step:
outputting the torch gas and the atomized desulfurized amine liquid in the pre-absorber to a compressor for compression;
and (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor enter a cooler, and are output after exchanging heat with a cold source input into the cooler;
a primary hypergravity desulfurization step:
inputting the cooled torch gas and the desulfurized amine liquid into a first hypergravity machine, contacting and transferring the torch gas and the desulfurized amine liquid in the first hypergravity machine to realize hypergravity desulfurization, and outputting the desulfurized torch gas from the first hypergravity machine;
a flash evaporation step:
flashing desulfurized amine liquid from the first hypergravity machine through a flash tank;
and (3) secondary hypergravity desulfurization:
and (3) inputting the torch gas output by the first hypergravity machine and the supplemented desulfurization amine liquid into a second hypergravity machine, contacting and transferring the torch gas and the desulfurization amine liquid in the second hypergravity machine to realize secondary hypergravity desulfurization, outputting the torch gas subjected to secondary hypergravity desulfurization from the second hypergravity machine, and atomizing and spraying the desulfurization amine liquid output by the second hypergravity machine into the pre-absorber.
According to a second embodiment of the invention, there is also provided a flare gas compression and desulfurization system, comprising a pre-absorber, a compressor, a cooler, a first hypergravity machine, a second hypergravity machine and a flash tank; the pre-absorber is provided with a flare gas inlet, a first amine liquid inlet, a second amine liquid inlet and an outlet; the first amine liquid inlet and the second amine liquid inlet are respectively provided with an atomizing nozzle so as to atomize the desulfurized amine liquid flowing into the first amine liquid inlet and the second amine liquid inlet and then spray the atomized desulfurized amine liquid into the pre-absorber; the inlet of the compressor is communicated with the outlet of the pre-absorber and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber; the cooler is provided with a cold side inlet and a cold side outlet for the cold source to enter and exit, and is used for carrying out heat exchange on the torch gas and the desulfurized amine liquid output by the compressor and the cold source; the first supergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the first supergravity machine, realizing supergravity desulfurization and outputting the desulfurized flare gas from a first outlet of the first supergravity machine; the first inlet of the second hypergravity machine is communicated with the first outlet of the first hypergravity machine, the second inlet of the second hypergravity machine is used for receiving supplemented desulfurization amine liquid, the second hypergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the second hypergravity machine, secondary hypergravity desulfurization is achieved, and the flare gas subjected to secondary hypergravity desulfurization is output from the first outlet of the second hypergravity machine; a second outlet of the second hypergravity machine is communicated with a second amine liquid inlet of the pre-absorber so as to output desulfurized amine liquid to the pre-absorber; and the inlet of the flash tank is communicated with the second outlet of the first hypergravity machine, and the flash tank is used for flashing the desulfurized amine liquid output by the first hypergravity machine.
The invention has at least the following advantages:
1. the investment cost is reduced. According to the embodiment of the invention, the desulfurized amine liquid is used as the spray liquid, meanwhile, the compression part is provided with the enhanced mass transfer equipment such as the pre-absorber and the supergravity machine, and the absorption process is completed in the compression part, so that an absorption tower is not required to be arranged, the process flow is simplified, and the floor area of the equipment is reduced;
2. the operation cost is reduced. Because the mass transfer effect is enhanced, the dosage of the desulfurization solution is reduced, the load of a pumping system is reduced, and the heat load of a regeneration system is reduced; the diesel oil consumption in the original compression process is saved;
3. because the gasification latent heat energy when the desulfurized amine liquid is injected into the inlet of the compressor reduces the temperature of the medium gas, the volume flow of the inlet of the compressor is reduced, and the heat load of the outlet cooler is reduced.
Drawings
FIG. 1 shows a schematic block diagram of a first embodiment of a flare gas compression and desulfurization system according to the present invention.
FIG. 2 shows a schematic block diagram of a second embodiment of a flare gas compression and desulfurization system according to the present invention.
Detailed Description
FIG. 1 shows a schematic block diagram of a first embodiment of a flare gas compression and desulfurization system according to the present invention. As shown in fig. 1, a flare gas compression and desulfurization system according to a first embodiment of the present invention includes a pre-absorber 1, a compressor 2, a cooler 3, a first hypergravity machine 41, and a flash tank 5.
The pre-absorber 1 has a flare gas inlet 11, an amine liquid inlet 12 and an outlet 13. The amine liquid inlet 12 is provided with an atomizing nozzle (not shown) for atomizing the desulfurized amine liquid (regenerated amine liquid in this embodiment) flowing into the amine liquid inlet 12 and spraying the atomized desulfurized amine liquid into the pre-absorber 1. By arranging the atomizing nozzle, the liquid drops of the amine liquid can reach the micron level, and the interphase mass transfer area is effectively enlarged.
The inlet 21 of the compressor 2 is communicated with the outlet 13 of the pre-absorber 1 and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber 1. In this embodiment, the compressor is an oil-free liquid spray screw compressor.
The hot side inlet 31 of the cooler 3 is communicated with the outlet of the compressor 2, the cooler 3 is further provided with a cold side inlet and a cold side outlet (not shown in the figure) for the cold source to enter and exit, and the cooler 3 is used for carrying out heat exchange on the flare gas and the desulfurized amine liquid output by the compressor 2 and the cold source.
The first inlet 411 of the first supergravity machine 41 is communicated with the hot side outlet 32 of the cooler 3, the second inlet 412 of the first supergravity machine 41 is used for receiving the desulfurization amine liquid input from the outside, the first supergravity machine 41 is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the first supergravity machine 41, the supergravity desulfurization is realized, and the desulfurized flare gas (namely, the purified gas shown in fig. 1, which is removed of hydrogen sulfide in a gas phase) is output from the first outlet 413 of the first supergravity machine 41.
The inlet 51 of the flash tank 5 is communicated with the second outlet 414 of the first hypergravity machine 41, and the flash tank is used for flashing the desulfurized amine liquid output by the first hypergravity machine 41. The flash evaporation 5 can remove light hydrocarbon gas and remove heavy hydrocarbon oil stains. The flash gas after flash evaporation is discharged from a first outlet 52 of the flash tank 5, and the rich amine liquid after flash evaporation is output from a second outlet 53 of the flash tank 5 and is sent to a regeneration system for regeneration.
The flare gas compression and desulfurization integrated process according to the first embodiment of the invention comprises the following steps:
A. a pre-desulfurization step:
the desulfurized amine liquid pumped by the regeneration tower (in the embodiment, the desulfurized amine liquid is MDEA solution, namely N-methyldiethanolamine solution) is atomized and sprayed into the pre-absorber 1, and is contacted with the flare gas from the gas holder in a reverse direction for mass transfer, so that pre-desulfurization is carried out. The minimum flow of the atomized amine liquid meets the liquid spraying amount required by cooling in the compression process.
In the embodiment, the pressure of the flare gas is 0.002-0.004 MPaG, and the temperature is 25-45 ℃; the concentration of hydrogen sulfide is 1-5% vol; the concentration of the desulfurized amine solution is 25-35 wt%, and the temperature is 35-40 ℃; the atomization pressure is 0.5-0.8 MPaG.
B. A compression step:
the flare gas and the atomized desulfurization amine liquid in the pre-absorber 1 enter the compressor 2 together, and are compressed in the compressor 2. The amine liquid plays a dual role in temperature reduction and desulfurization in the process, and mass transfer is enhanced in the process of violent disturbance and pressure rise of a compressor rotor. In the embodiment, the outlet pressure of the compressor is 0.6-0.8 MPaG.
C. And (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor 2 enter the cooler 3, and are output after exchanging heat with the cold source input into the cooler 3.
In this embodiment, the cooler 3 is a U-tube heat exchanger, the cold source is cooling water, and the gas-liquid two-phase mixture of the flare gas and the desulfurized amine liquid is cooled to about 40 ℃. In the cooler 3, the gas-liquid two-phase mixture passes through the tube side, the cooling water passes through the shell side, and the gas-liquid two-phase mixture continues to carry out mass transfer in the pipeline.
D. A hypergravity desulfurization step:
and (3) enabling a gas-liquid two-phase mixture of the compressed and cooled torch gas and the desulfurization amine liquid to enter the first hypergravity machine 41, simultaneously atomizing and spraying a supplemented stream of the desulfurization amine liquid into the first hypergravity machine 41, and enabling the torch gas and the desulfurization amine liquid to be in contact mass transfer in the first hypergravity machine, so that the hypergravity desulfurization is realized.
In this step, the first supergravity machine 41 may select a counter-current mass transfer mode or a parallel-current mass transfer mode (the conventional supergravity machine has two modes of counter-current mass transfer and parallel-current mass transfer). Under the parallel flow mass transfer mode, the desulphurization amine liquid in the original flare gas and the supplemented desulphurization amine liquid simultaneously flow and contact with the flare gas in the same direction for mass transfer; under the condition of countercurrent mass transfer, only the supplemented desulfurization amine liquid and the flare gas flow in a reverse direction to contact and transfer mass, the desulfurization amine liquid in the original flare gas is separated by gravity after entering the hypergravity machine, and the desulfurization amine liquid after completing the contact and mass transfer with the flare gas and the desulfurization amine liquid in the original flare gas are both output from the second outlet 414 of the first hypergravity machine 41.
In the first high-gravity machine 41, the desulfurized amine liquid is stretched into liquid drops, liquid films or liquid filaments by huge centrifugal force, so that the contact area between phases is effectively increased, and the mass transfer is strengthened.
E. A flash evaporation step:
the rich amine liquid from the first hypergravity machine 41 enters a flash tank 5, light hydrocarbon gas is removed through flash evaporation, and heavy hydrocarbon oil stains are skimmed. And the amine-rich liquid after flash evaporation is sent to a regeneration system for regeneration, so that cyclic utilization is realized. In this embodiment, the desulfurized amine liquid atomized and injected into the pre-absorber 1 and the first high-gravity machine 41 are both regenerated desulfurized amine liquids.
FIG. 2 shows a schematic block diagram of a second embodiment of a flare gas compression and desulfurization system according to the present invention. As shown in fig. 2, a flare gas compression and desulfurization system according to a second embodiment of the present invention includes a pre-absorber 1A, a compressor 2, a cooler 3, a first hypergravity machine 41, a second hypergravity machine 42, and a flash tank 5.
The pre-absorber 1 has a flare gas inlet 11, a first amine liquid inlet 12, an outlet 13, and a second amine liquid inlet 14. The first amine liquid inlet 12 and the second amine liquid inlet 14 are respectively provided with an atomizing nozzle (not shown) to atomize the desulfurized amine liquid flowing into the first amine liquid inlet 12 and the second amine liquid inlet 14 and then spray the atomized desulfurized amine liquid into the pre-absorber 1.
The inlet 21 of the compressor 2 is communicated with the outlet 13 of the pre-absorber 1 and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber 1. In this embodiment, the compressor is an oil-free liquid spray screw compressor.
The hot side inlet 31 of the cooler 3 is communicated with the outlet of the compressor 2, the cooler 3 is further provided with a cold side inlet and a cold side outlet (not shown in the figure) for the cold source to enter and exit, and the cooler 3 is used for carrying out heat exchange on the flare gas and the desulfurized amine liquid output by the compressor 2 and the cold source.
The first inlet 411 of the first hypergravity machine 41 is communicated with the hot side outlet 32 of the cooler 3, and the first hypergravity machine 41 is used for enabling the flare gas and the desulfurized amine liquid to contact and transfer mass in the first hypergravity machine 41, realizing hypergravity desulfurization, and outputting the desulfurized flare gas from the first outlet 413 of the first hypergravity machine 41.
The first inlet 421 of the second supergravity machine 42 is communicated with the first outlet 413 of the first supergravity machine, the second inlet 422 of the second supergravity machine 42 is used for receiving supplementary desulfurized amine liquid (regenerated amine liquid in this embodiment), the second supergravity machine 42 is used for contacting and transferring the flare gas and the desulfurized amine liquid in the second supergravity machine, so as to realize secondary supergravity desulfurization, and the flare gas after the secondary supergravity desulfurization (i.e. the purified gas shown in fig. 2, which removes hydrogen sulfide in a gas phase) is output from the first outlet 423 of the second supergravity machine 42; the second outlet 424 of the second hypergravity machine 42 is communicated with the second amine liquid inlet 14 of the pre-absorber 1 to output the desulfurized amine liquid to the pre-absorber 1.
The inlet 51 of the flash tank 5 is communicated with the second outlet 414 of the first hypergravity machine 41, and the flash tank 5 is used for flashing the desulfurized amine liquid output by the first hypergravity machine 41. The flash evaporation 5 can remove light hydrocarbon gas and remove heavy hydrocarbon oil stains. The flash gas after flash evaporation is discharged from a first outlet 52 of the flash tank 5, and the rich amine liquid after flash evaporation is output from a second outlet 53 of the flash tank 5 and is sent to a regeneration system for regeneration.
The flare gas compression and desulfurization integrated process according to the second embodiment of the present invention comprises the steps of:
A. a pre-desulfurization step:
the first path of desulfurized amine liquid (regenerated amine liquid in this embodiment) and the second path of desulfurized amine liquid from the second hypergravity machine 42 are respectively atomized and sprayed into the pre-absorber 1A, and reversely contacted with the flare gas introduced into the pre-absorber 1A from the gas holder for mass transfer, so as to perform pre-desulfurization.
B. A compression step:
the flare gas and the atomized desulfurized amine liquid in the pre-absorber 1A are output to the compressor 2 together for compression.
C. And (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor 2 enter the cooler 3, and are output after exchanging heat with the cold source input into the cooler 3.
In this embodiment, the cooler 3 is a U-tube heat exchanger, the cold source is cooling water, and the gas-liquid two-phase mixture of the flare gas and the desulfurized amine liquid is cooled to about 40 ℃. In the cooler 3, the gas-liquid two-phase mixture passes through the tube side, the cooling water passes through the shell side, and the gas-liquid two-phase mixture continues to carry out mass transfer in the pipeline.
D. A primary hypergravity desulfurization step:
the compressed and cooled gas-liquid two-phase mixture of the flare gas and the desulfurized amine liquid enters the first hypergravity machine 41, the flare gas and the desulfurized amine liquid contact and transfer mass in the first hypergravity machine to realize hypergravity desulfurization, and the desulfurized flare gas is output from the first hypergravity machine 41. The first hypergravity machine 41 can select a counter-current mass transfer mode or a parallel-current mass transfer mode.
E. A flash evaporation step:
the rich amine liquid from the first hypergravity machine 41 enters a flash tank 5, light hydrocarbon gas is removed through flash evaporation, and heavy hydrocarbon oil stains are skimmed. And the amine-rich liquid after flash evaporation is sent to a regeneration system for regeneration, so that cyclic utilization is realized.
F. And (3) secondary hypergravity desulfurization:
inputting the torch gas output by the first hypergravity machine and the supplemented desulfurization amine liquid (regenerated amine liquid in the embodiment) into a second hypergravity machine 42, contacting and transferring the torch gas and the desulfurization amine liquid in the second hypergravity machine to realize secondary hypergravity desulfurization, and outputting the torch gas subjected to secondary hypergravity desulfurization from the second hypergravity machine to enter a fuel gas pipe network; the desulfurized amine liquid output by the second hypergravity machine 42 is atomized and sprayed into the pre-absorber 1A. The second hypergravity machine 42 can select a counter-current mass transfer mode or a parallel-current mass transfer mode.
One of the main differences between the second embodiment and the first embodiment is the addition of a secondary supergravity desulfurization step, making the second embodiment suitable for the desulfurization recovery of flare gas with a higher hydrogen sulfide content. The content of hydrogen sulfide in the flare gas desulfurized by the first hypergravity machine is greatly reduced, and the amine liquid separated by the second hypergravity machine is introduced into the pre-absorber, so that the use amount of the amine liquid can be greatly reduced, and the regeneration load of the amine liquid is further reduced. If the desulfurization effect of the first hypergravity machine can meet the design requirement, the second hypergravity desulfurization is not needed.
The invention adopts the desulfurized amine liquid as the spray liquid, and simultaneously arranges the pre-absorber, the hypergravity machine and other strengthening mass transfer equipment at the compression part, and completes the absorption process at the compression part, thereby not needing to arrange an absorption tower, simplifying the process flow, reducing the occupied area of the equipment and improving the desulfurization efficiency.
Claims (10)
1. A flare gas compression and desulfurization integrated process is characterized by comprising the following steps:
a pre-desulfurization step:
atomizing and spraying the desulfurized amine liquid into a pre-absorber, and contacting and transferring mass with torch gas introduced into the pre-absorber to perform pre-desulfurization;
a compression step:
outputting the torch gas and the atomized desulfurized amine liquid in the pre-absorber to a compressor for compression;
and (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor enter a cooler, and are output after exchanging heat with a cold source input into the cooler;
a hypergravity desulfurization step:
inputting the cooled flare gas, the desulfurized amine liquid and the supplemented desulfurized amine liquid into a first hypergravity machine, contacting and transferring the flare gas and the desulfurized amine liquid in the first hypergravity machine to realize hypergravity desulfurization, and outputting the desulfurized flare gas from the first hypergravity machine;
a flash evaporation step:
and (3) flashing the desulfurized amine liquid from the first hypergravity machine through a flash tank.
2. The process of claim 1, wherein in the step of super-gravity desulfurization, additional desulfurized amine liquid is atomized and injected into the first super-gravity machine.
3. The flare gas compression and desulfurization process of claim 1, wherein the desulfurized amine solution is a solution of N-methyldiethanolamine.
4. A flare gas compression and desulfurization system is characterized by comprising a pre-absorber, a compressor, a cooler, a first hypergravity machine and a flash tank;
the pre-absorber is provided with a flare gas inlet, an amine liquid inlet and an amine liquid outlet; the amine liquid inlet is provided with an atomizing spray head so as to atomize the desulfurized amine liquid flowing into the amine liquid inlet and then spray the desulfurized amine liquid into the pre-absorber;
the inlet of the compressor is communicated with the outlet of the pre-absorber and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber;
the cooler is provided with a cold side inlet and a cold side outlet for the cold source to enter and exit, and is used for carrying out heat exchange on the flare gas and the desulfurized amine liquid output by the compressor and the cold source;
the first inlet of the first hypergravity machine is communicated with the hot side outlet of the cooler, the second inlet of the first hypergravity machine is used for receiving supplemented desulfurization amine liquid, the first hypergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the first hypergravity machine, the hypergravity desulfurization is realized, and the desulfurized flare gas is output from the first outlet of the first hypergravity machine;
and the inlet of the flash tank is communicated with the second outlet of the first hypergravity machine, and the flash tank is used for flashing the desulfurized amine liquid output by the first hypergravity machine.
5. The flare gas compression and desulfurization system of claim 4, wherein the compressor is an oil-free spray screw compressor.
6. A flare gas compression and desulfurization integrated process is characterized by comprising the following steps:
a pre-desulfurization step:
respectively atomizing and spraying the first path of desulfurized amine liquid and the second path of desulfurized amine liquid from a second hypergravity machine into a pre-absorber, and contacting and transferring mass with torch gas introduced into the pre-absorber to perform pre-desulfurization;
a compression step:
outputting the torch gas and the atomized desulfurized amine liquid in the pre-absorber to a compressor for compression;
and (3) cooling:
the torch gas and the desulfurized amine liquid output from the compressor enter a cooler, and are output after exchanging heat with a cold source input into the cooler;
a primary hypergravity desulfurization step:
inputting the cooled torch gas and the desulfurized amine liquid into a first hypergravity machine, contacting and transferring the torch gas and the desulfurized amine liquid in the first hypergravity machine to realize hypergravity desulfurization, and outputting the desulfurized torch gas from the first hypergravity machine;
a flash evaporation step:
flashing desulfurized amine liquid from the first hypergravity machine through a flash tank;
and (3) secondary hypergravity desulfurization:
and (3) inputting the torch gas output by the first hypergravity machine and the supplemented desulfurization amine liquid into a second hypergravity machine, contacting and transferring the torch gas and the desulfurization amine liquid in the second hypergravity machine to realize secondary hypergravity desulfurization, outputting the torch gas subjected to secondary hypergravity desulfurization from the second hypergravity machine, and atomizing and spraying the desulfurization amine liquid output by the second hypergravity machine into the pre-absorber.
7. The integrated flare gas compression and desulfurization process of claim 6, wherein in the secondary hypergravity desulfurization step, additional desulfurized amine liquid is atomized and injected into the second hypergravity machine.
8. The integrated flare gas compression and desulfurization process of claim 6, wherein the desulfurized amine solution is a solution of N-methyldiethanolamine.
9. A flare gas compression and desulfurization system is characterized by comprising a pre-absorber, a compressor, a cooler, a first hypergravity machine, a second hypergravity machine and a flash tank;
the pre-absorber is provided with a flare gas inlet, a first amine liquid inlet, a second amine liquid inlet and an outlet; the first amine liquid inlet and the second amine liquid inlet are respectively provided with an atomizing nozzle so as to atomize the desulfurized amine liquid flowing into the first amine liquid inlet and the second amine liquid inlet and then spray the atomized desulfurized amine liquid into the pre-absorber;
the inlet of the compressor is communicated with the outlet of the pre-absorber and is used for compressing the torch gas and the atomized desulfurized amine liquid output by the pre-absorber;
the cooler is provided with a cold side inlet and a cold side outlet for the cold source to enter and exit, and is used for carrying out heat exchange on the flare gas and the desulfurized amine liquid output by the compressor and the cold source;
the first supergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the first supergravity machine, so that supergravity desulfurization is realized, and the desulfurized flare gas is output from the first outlet of the first supergravity machine;
the first inlet of the second hypergravity machine is communicated with the first outlet of the first hypergravity machine, the second inlet of the second hypergravity machine is used for receiving supplemented desulfurization amine liquid, the second hypergravity machine is used for enabling the flare gas and the desulfurization amine liquid to contact and transfer mass in the second hypergravity machine, secondary hypergravity desulfurization is achieved, and the flare gas subjected to secondary hypergravity desulfurization is output from the first outlet of the second hypergravity machine; a second outlet of the second hypergravity machine is communicated with a second amine liquid inlet of the pre-absorber so as to output desulfurized amine liquid to the pre-absorber;
and the inlet of the flash tank is communicated with the second outlet of the first hypergravity machine, and the flash tank is used for flashing the desulfurized amine liquid output by the first hypergravity machine.
10. The flare gas compression and desulfurization system of claim 9, wherein the compressor is an oil-free spray screw compressor.
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